Process for making motor fuel



2 Sheets-Sheet l mmmmlw M mwwwl B. FIXMAN PROCESS FOR MAKING MOTOR FUEL Filed Nov,

:1M l l I Irv ....fflumr ll Ilm Nov. 18, 1930.

NOV. 18, 193). B FlxMAN n 1,781,872

PROCESHS FOR MAKING MOTOR FUEL Filed Nov. 18, 1926 2 Sheets-Sheet' 2 IM/ouate@ lEmliTLv F-'Lxman bons of lower molecular weight, such as gaso Patented Nov. 18, 1930 UNITED STATES.

BENJAMIN FIXMAN, 0F IBARTLESVIILE, KLAHOMA PROCESS FOR MAKING- MOTOR FUEL I Application led November 18,w1926. Serial No. 149,195.

This invention relates to improvements in processes for converting hydrocarbons of high molecular weight, such as heavy mineral oils, and residual products, into hydrocarline or motor fuel for automotive internal combustion engines.

The primary object of the invention is the provision of an improved process for `carry- Tt ing out the process, for a continuous and practically quantitative conversion of hydrocarbons of high molecular weight into hydro carbons of lower molecular weight.

A further object of this invention is the l provision ofmeans for initiall treating a raw oil in such manner that t e optimum conversion temperature is .maintained independent of the heat treatment of a recycle stock, which is independently treated under favorable pressure and temperature conditions, so that the raw oil and recycle oil after such treatments may be intermingled in an equilibrium chamber under the most favorable conditions.

A further object of this invention is the provision of process for recoverin a maximum" yield of gasoline or motor uel from hydrocarbon oils, which includes the independent heat and pressure treatment of raw and recycle oils in such a relation that the optimum temperature conditions may be obtained, and subsequently mixin the heated products and removing carbon y preci itation and electroma etic treatment o the same in the vapor p ase so as to prevent the contamination of residual oils with carbon and enable the conversion of the ultimate percent of desired fraction within a single system without excessive losses in the formation of carbon and fixed gases.

Other objects andadvantages of this invention will be apparent duringthe course of the following detailed description.L

a part of this specication, and wherein similar reference characters designate corresponding parts throughout the several views,

Figure 1 is a diagrammatic representation of the apparatus 1n which the improved processis carried out.

Figure 2 is a sectional view taken substantially on the line 2-2 of Figure 1. l

' Figure 3 is a fragmentary vertical sectional view taken through the lower portion of the equilibrium chamber.

Figure 4 is a sectional view tially on the line 4 4 of Figure 6.

Figure 5 is a bottom plan View of an upper spray head used to s ray the initially treated raw oil into the equi ibrium chamber.

Figure 6 is a side elevation `of the spray head illustrated in Figure 5.

Figure 7 is a horizontal sectional view. taken substantially on the line 7 7, of Figure l, through the carbon precipitator.

"Figure 8 is a vertical sectional view taken through the lower portion of the rejecting 1 column of the apparatus, showing more particularly float means for regulating the forced pumping of recycle oil from the rejecting column.

Figure 9 is a plan view of details illustrated in Figure 8.

Figure 10 is a sectional view showing the mollinting of the ioat in the rejecting column tan In the drawings, wherein for the purpose of illustration is shown onlya preferred embodiment of this invention, the letter A may generally designate a primary converter' or still in which raw oil is treated; B a secondary converter or still in which the recycle oil ber C E a rejecting column wherein the products are received after treatment in the cipitator D, and from whence the more volatile fractions pass, preferablyy in vapor phase through a tubular dephlegmator H an 'p thence into a condenser F, and'tank G; the In the accompanying drawings, forming In the preferred procedure, the raw mini eral oil, suchas fuel oil, to beconverted is caused toow from any suitable source into the optimum temperature, which is character.

the pipe 15, and is forced by a ump 16 under pressure through a pipe 17, t rough the dephlegmator H, and out through a conduit 18 and thence into the lower portion of the coil 20 of the primary converter or still A; this coil 20 bein of the continuous type, andbeing externa y heated by hot luevgases in any approved manner. In the primary converter the raw mineral oil undergoes conversion at istic of the raw mineral oil at which the molecular structure thereof becomes unstable and cracking occurs without excessive loss complications resulting from a combined rerun treatment, and therefore the optimum temperature and pressure relation maybe carried out. The heated raw mineral oil, in liquid phase, passes from the converter A thru the conduit 22 into a spray head 23 located in the equilibrium chamber C, intermediate the top .and bottom thereof, from whence the same is sprayed in the relation to be subsequently described The equilibrium receptacle 25 is of the vertical elongated.y type, providin a compartment 26, wherein the spray hea 23 is mounted, above the bottom 27 of the equilibrium receptacle. This spray .head 23 is of any approved type, preferably providing a plurahty of intercommunicating concentric rings 29, such as shown in `Figure '5 of the drawings, the lower surfaces of which are provided with downwardly extending nozzles 30 provided with passageways therethrough which are restricted at' 31 adjacent their outlets. The heated ,raw i'xineral oil, in liquid phase, 1s sprayed froiiithespra7 head 23, downward- 1y, in the lower half o the equilibrium compartment 26, and is sprayed into a mass of similar oil undergoing conversion at substantially the same temperature. The equilibrium chamber is maintained under pressure enerated by the heat of materials entere same, of suilicient intensity to keep in Y in t v a Iiquid state the substantial portion of the cated hydrocarbons which have unstable molecular structures at the temperature maintained int of entry from the primary conat the g verter The equilibrium chamber compartment 26 is provided withtperforated conical bailles 35 and 36, below e spray head 23, onto which the oil from the spray head is ejected to substantially film' out the same and insure a uniform treatment of the sam with the upwardly lowinghot vapors f ro the lower spray head 38 ,which will be subsequentl mentioned. 'lhe spray head 3 8 is lolow the bafes 35 and 36, and dis-v penses hot oil inthe vapor. phase from' the secondary converter B, so as to keep the vapors,

. liquid, and solid reaction products in a state end of the carbon precipitator D, thru'a flared distributor 42, which is preferably located concentrically in the upper end of the compartment 41 of the carbon precipitator D.

In the upper end of the equilibrium chambervC, above the spray head 23, a plurality of perforated baffles 45 may be located, to properly intermingle and mix the products in the compartment 26, as they arise thru the conduit 40, `from whence the hydrocarbon products for the carbon precipitator D are withdrawn. l

'A pressure is maintained in the carbon precipitator D, lower than the pressure of reaction in the equilibrium chamber C; the difference in pressures being regulated by the valves 41.

The fact that the hydrocarbons or homogeneous mixture lof reaction products, which consists in a large part of superheated vapors carryin a small percentage of liquid by mechanic entrainment, and elementary carbon car n precipitator D at a lower temperature, insures that the same will assume entirely the vapor phase, excepting of course the elementar carbon and any adsorbed tars.

The carbon precipitator D includes the vertically disposed vsubstantiallv cylindrical shaped receptacle 50, in the top 51 of which the ared distributor 42 is mounted, and which at the bottom thereof may be provided with a manhole 52 or the like. A hollow cylindrical shaped positive electrode 53 is supportedconcentrically in the carbon precipitator receptacle 50, the same being open at the top and bottom thereof for free passage of the vapor products, and preferably axially in this positive electrode cylinder 53, is supported anega-tive electrode 55, immediately below the lia-red distributor 42. The vapors passthru the electromagnetic field created by the electrodes 53 and 55,'rst passing downwardly around the negative electrode 55, and tnence reversing their direction at the bottom of the carbon preci itator and passing upwardly and tangenti y pass out of the carbon precipitator thru a conduit v57.

In passing thru th electro-magnetic iield I the elementary carbon-is precipitated from the vapors and-accumulated within the carbon precipitator, and the vapors pass thru the conduit 5.7 into the intermediate portion of the re]ecting column E, and thence upwardly suspgnded in the liquid, is expanded into the iso thru suitable devised and approved scrub bing trays 58, and the vapor fraction escapes from the rejecting column, thru a .passageway 59 in the top thereof, into the tubular de'- `phlegmator from whence the same exits thru a conduit 60 and passes into the "conv denser F. v In the oil cooled dephlegmator H,

as well as in the scrubbing trays58, the un-` converted hydrocarbons L are precipitated from the vapor stream, ein the liquid phase, and this rejected liquid passes counter current to the ascending vapor stream, and settle in a body of liquid 62 in the lower portion of the rejecting column, as is illustrated in Figures 1 and 8 of the drawings.

The incompletely converted hydrocarbons accumulating in the'lower portion of the rejecting column E may be conveniently termed the recycle stock, and the same is discharged thru a conduit 65, and force pumped by a pump K into a conduit 66 and thence into the continuous coil 67 of the secondary converter or still B. In the secondary converter B, the

recycle stock is externally. heated in the coil 67 by hot flue gases. A regulated pressure is maintained in the coil 67 by means of a pressure re ulating'valve 68 located at the end of the coi 67 opposite the conduit 66, to permit heating of the recycle oil under optimum temperalture and pressure conditions, to enable the proper conversion of the same under circumstances which enables the molecules to becom l unstable and crack. The heated recycle stock after passingthe valve 68 is dis- .72 into the lower end of the equilibrium receptacle compartment 26, by means of the spray head 38. This spray head 38 is formed as more particularly illustrated in Flgure 3 of the drawings, having the nozzles 7 5 thereof.

directed downwardlytowards the bottom 27 of the equilibrium chamber 25, and the vapor phase product as sprayed from the spray head 38 arises, and the reaction products from the recycle stock are caused to mix uniformly with the reaction products from the raw mineral oil which has been sprayed thru the .spray head 23, as above mentioned,"and this isI accomplished by means of the upper parallel ow of all reaction products in their baffled relation. v

By means of the intimate prolonged contact between reaction products from the raw mineral oil and recycle stock, as accomplished charged thrua conduit 69 into a. superheating j `in the equilibrium Chamber 0,5111 'advantage is derived from thermo-catalytic synthesis or constructive conversion at elevated temperatures, or association of molecular structures a well as to the crackingreaction or dissoci-atisdn of molecular structures at elevated temperatures.

As to the means of controlling the operation of the pump K, .a float 80 is supported at the free end of the float arm 81; the latter being mounted on a shaft 82 which is rotatably supported in a suitable tube 83 eX- tending transversely through' the tank or column E as is illustrated in Figure 10 of the drawings. The shaft 82, at the end extending into the rejecting column E and has thel arm 81 rigidly mounting thereon, and at the opposite end exteriorly of the column is rigidly provided with an outwardly extending arm 85 which supports a counter weight 86 at the outer end thereof. Intermediate its ends the arm 85 has a dependingV connecting rod 88 which operates a slide valve 89 controlling the admission of steam or other operating medium, from the line 90 to the engine 91. Since the engine is'electrically operated, the arm 88 nay of course operate a switch instead of the valve 89. (Qlf course the 'engine 91 is for operating the pump K, and upon elevation of the liquid to a proper level the valve will be open for setting the engine 91' in operation and conv sequently operate the pump K for pumping the recycle stock 62 from the rejecting column E into the secondary converterior stillv B. Lubrication of the shaft 82 in-tlie sleeve 83 may be effected by forcing oil under pressure thru a conduit 92; this conduit 92 receiving a pressure supply of cold raw oil from the conduit 17, in the relation of parts illustrated in Figure 1 of the drawings.

Referring more in detail to the process and parts of the apparatus thereof, the temperaturefof'the raw oil leaving the primary converter A is of course governed by its composition, and the treatment of the same in vthe various parts of the apparatus is of course proportionately" regulated. By way ofexample, operating characteristics for a ratio of recycle oil to raw oil, of 5 to 1, inl the case of virgin mid-continent raw oils, may be as follows: i

- Al'gtgl' Temperature Pressure Ilessu mw oil en recycle oil lbs. sq. Shag: Gravity raw oil term e ui entering in. within m' Wt) l Hbugl equilibrium equilibrigci tank tank um tank tatot.

18-24 750 F770 F. 800 F820 F. 125-150 30-50 24-30 770 F.790 F. 820 :Fr-840 F. 150-175 50-75 30-36 7m Frlo F. 840 F.860 F. 175-250 'f5-150 The heat treatment within the converter B, of the recycleV oil is carried out iu two steps,vnamely, a first heating done in the furnace coil 67,. wherein the recycle oil is Aheated under sufficient pressure to keep it substantially in the liquid phase. As the oil 'passes valve 68 it expands and assumes subto the superheated coil 70 which adds the re! quired temperature head for causing the reaction in the equilibrium chamber C.

I` have found that the temperature differential/between the recycle 011 entering the tank C and the raw oil enteri tank C, that is necessary to supply the latent heat of the raw oil and the endothermic heat of conversion is about correc-t to establish the recycle oil at its optimum conversion temperature when the ratio of recycle oil to raw oil is substantially 5 to 1. However, the ratio of recycle oil to raw oil can be raised or lowered with a corresponding reverse movement of said temperature differential until for a given optimum temperature of the raw oil, the optimum temperature will be obtained for the recycle oil entering the tank C. It is therefore evident that the ressure carried in the tanky C and in the Jcar on precipitator are both functions of the ratio of recycle oil to raw oil, and hence I do not Wish to be limited to the operating pressures above designated, as these apply merely to raw oil from a particular source. An oil d of the equilibrium tank C maintained as the v hottest zone. The unconverted hydrocarbons 4of highest molecular weight of course rewhich may be a by-product of other conversion processes or produced from other sources may be of quite dilferent character and require different temperature and ratios of recyclel oil to raw oil.

It ive important to have the lower part main in the liquid phase in tank C andpasses downwardly over the baiiles, to approach the highest temperature zones, where they can by reason of the higher temperature morek easily undergo conversion, and of course part of the liquid may be entrained by the arising vapors, and in this connection the perfo.

rated baffles are important. In order that conversionmay becarried' out, the time factor of reaction must be considered, and the principle of the arrangement in the equilibrium chamber permits the fullest realizationA of radvantages of the timel factor, since the heated raw oil in liquidfphase and the heated l recycle oil in vapor phase are admitted to /liqui into vapor'at a reduced pressure. As

the percentage of entrained liquid is small compared withthe Weight of yapors, the temperature drop is correspondingly small.

While the 'above table gives the relative difference of pressures between the tanks C andV D, these temperatures may vary considerably, and I elect to operate with a minimum pressure drop between the tanks C and D.

The pressure in the rejecting column E may be substantially about 30 pounds, but this may vary, and in this connection the pressures in the tanks D and E are substantially the same.

While the vapors as they pass into the re-s jecting column are not heated by any appa ratus illustrated in the drawings, yet a certain degree of rectification is obtained. in the column E by bringing `the ascending vapors into the tank E under the lowest drop tray, and if desired the recycle oil which collects in the bottom of the rejectingy column may be heated so as to rectify the condensed recycle oil still further.

The condensate in F is stored in a suitable reservoir G. y

If desired, a heat exchange device may be placed in the conduit 57 between the precipitator and column E. and through which the y recycle o'l of conduit 66 may pass to heat said recycle oil in. a counter current flow to the hot vapors passing thru the conduit 67.

Various changes in the shape, size, arrangement of parts, as well as in the steps of the process, may be made to the form of invention herein shown and described, without departing from the spirit of the invention ory the scope of theclaims.

I claim:

1. The process of producing hydrocarbons of substantially the character of motor fuels which consists in heating a raw heavy mineral oil to the conversion temperature under pres-- sure, heating a recycle oil, intimately contacting the heated heavy mineral oiland the reaction products resulting therefrom with the separately heated recycle oil, releasing the resultant hydrocarbon mixture at a reduced pressure which will enable liquid components of the mixture to vaporize, removing carbon from thevaporby electro-magnetic treatment, and separating the hydrocarbons of the desired characteristics from those requiring recycling to produce the recycle oil above mentioned. 0

2. A process. of mineral oil conversion, which consistsin heating to"conversion temperature a primary body of hydrocarbon maintained in substantially liquidl phase, sprayingthe reaction mass so produced` into -a pressure equilibrium zone aboveV a heat dry vapors so produced and freed from solid impurities to obtain a desired vapor fraction and a liquid recycle stock, heating the liquid recycle stock while maintained in substantially liquid phase to conversion temperature, vaporizing the recycle stock so heated by expanding it into a heated zone of lower pressure, reheating the recycle stock vapors to restore the conversion temperature existing prior to vaporization, and spraying the said heated recycle stock vapors at conversion temperature into the pressure equilibrium zone first mentioned, said recycle stock vapors at conversion temperature being the heat treated secondary body of hydrocarbon mentioned above.

8. The process of producing hydrocarbons of substantially the character of motor fuels which consists in heating under pressure a primary heavy mineral oil to conversion temperature, separately heating to conversion temperature a recycle oil under higher pressure than the pressure used for the primary oil, reducing the pressure on the recycle oil to substantially the pressure maintained on the primary oil to vaporize the same, reheat- 'ing the recycle oil vapors so produced to the conversion temperature attained prior to the 'reduction of pressure, causing the conversion masses of primary and recycle oil to enter a pressure equilibrium zone with the primary oil entering above the point of entry of the conversion mass of recycle oil admitted to the pressure equilibrium zone, regulating the ratio of primary and recycle oils entering the equilibrium zone to prevent a substantial tem perature dierential between the primary conversion mass before and after entering the 'equilibrium zone, withdrawing the resultant hydrocarbon mixture from the top of the equilibrium zone, releasing the pressure to enable entrained liquid components to-vapor ize, removing carbon from the vapor by means of an electrical eld, and ractionating the hydrocarbons of the desired characteristics from those requiring recycling to produce the y recycle oil above mentioned.

BENJAMIN FIXMAN. 

